EP1077085B1 - Précarbonation de catalyseur d'hydrotraitement - Google Patents
Précarbonation de catalyseur d'hydrotraitement Download PDFInfo
- Publication number
- EP1077085B1 EP1077085B1 EP00402216A EP00402216A EP1077085B1 EP 1077085 B1 EP1077085 B1 EP 1077085B1 EP 00402216 A EP00402216 A EP 00402216A EP 00402216 A EP00402216 A EP 00402216A EP 1077085 B1 EP1077085 B1 EP 1077085B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- catalyst
- process according
- containing compound
- impregnation
- hydrogen
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/02—Sulfur, selenium or tellurium; Compounds thereof
- B01J27/04—Sulfides
- B01J27/047—Sulfides with chromium, molybdenum, tungsten or polonium
- B01J27/051—Molybdenum
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/08—Heat treatment
- B01J37/082—Decomposition and pyrolysis
- B01J37/084—Decomposition of carbon-containing compounds into carbon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/20—Sulfiding
Definitions
- Hydrotreating catalysts generally comprising an amorphous or crystalline oxide support such as, for example, an alumina, a silica or a silica-alumina, a zeolite on which at least one element from groups VIII and VI of the periodic table or a combination of several elements from these same groups, such as solids designated CoMo / Al 2 O 3 , NiMo / Al 2 O 3 or NiW / Al 2 O 3 must be previously sulphurized to give them catalytic performance for all reactions hydrotreating, for example hydrodesulfurization, hydrodenitrogenation, demetallation and certain hydrogenations.
- This pre-catalytic sulphidation step can be carried out in two different ways.
- the first, so-called in-situ sulphidation which is characterized by the fact that the catalyst in its oxide form is first charged to the hydrocarbon conversion reactor to be sulfurized therein.
- the second said off-site presulphurization as described in various patents of the applicant (USP4719195, USP 5397756, EP-A 785022) differs from the previous one by the fact that the sulfurization or Presulfurization of the catalyst is carried out in a separate unit distinct from the reactor hydrotreating.
- the object of the present invention is to proceed with the implementation of the presulphurization of the catalyst by presence of hydrogen and at least one sulfur compound which may be hydrogen sulfide or any other sulfur compound capable of generating hydrogen sulphide by hydrogenolysis, characterized in in order to improve the catalytic performances in the hydrotreatment reactions, the
- the catalyst is precarbonized so as to deposit solid carbon in the pores of the catalyst. most non-leachable.
- the process according to the invention is particularly applicable to a presulphurization performed off site.
- the present invention characterized by the use of precarbonation, makes it possible to improve hydrodesulphurizing and hydrogenating properties of the catalyst.
- this precarbonation makes it possible to reduce the initial selectivity in cracking and isomerization product.
- a explanatory hypothesis may be that this decrease in selectivity in cracking and isoménsation is due to that the carbon deposit attenuates the acidity of the support. The deactivation of the catalyst can thus be decreased and its lifespan increased.
- Precarbonation is carried out prior to the presulphuration phase.
- the liquid carbon compound is introduced in the porosity of the catalyst without necessarily aiming at the total filling of the pore volume of the catalyst. It is therefore a partial filling of the impregnation volume between 10% and 100% and preferably between 20 and 90%.
- Suitable carbon sources may be selected from paraffinic, naphthenic and / or aliphatic hydrocarbons, but also among the compounds oxygenated organic compounds such as alcohols, ketones, aldehydes, organic acids, fatty acids and vegetable oils. These compounds are characterized by high boiling points as for example between 150 ° C and 500 ° C and preferably above 200 ° C.
- the amount of carbon deposited at the end of the impregnation stage is between 2% and 30% by weight relative to the mass of oxide catalyst.
- a heat treatment step is necessary, this step of heat treatment being carried out under nitrogen or another inert gas, at a temperature between 150 ° C and 650 ° C and preferably between 300 ° C and 500 ° C.
- the purpose of this post heat treatment, or Pyrolysis, preferably carried out under inert gas is twofold.
- Its function is, on the one hand, the readjustment of the carbon content between 2% and 10% by weight and preferably between 3% and 7% by weight relative to the matrix oxide, and secondly the transformation of hydrocarbons, oxygenated or not, introduced during the stage impregnation, so that the residual carbon, at a content between 2% weight and 10% weight and preferably between 3% by weight and 7% by weight relative to the oxide, ie a carbon compound Most of the residue is non-leachable with toluene at reflux.
- the residual carbon compound is in the major non-leachable part with toluene at reflux, that is to say that the leaching rate is less than 40%, preferred way less than 30% and even more preferably less than 20%.
- the precarbonation can also be carried out by direct reaction between the solid and a hydrocarbon compound. It is possible to use a compound which is ready to polymerize, for example olefins or diolefins at a temperature between 20 and 400 ° C.
- the step of sulphurizing the precarbonated catalyst can be carried out at atmospheric pressure in a reactor heated between 200 ° C and 600 ° C, preferably between 200 ° C and 500 ° C, in the presence of a mixture gaseous sulfo reducer. More particularly, the method according to the invention applies to sulfurizations off-site that can be done at high temperatures, for example at temperatures above 400 ° C.
- the reactor used may be a fixed bed reactor or a system using the technology mobile bed such as the rotating bed, the fluidized bed or the crumbling bed.
- the sulpho gas mixture reductant consists of hydrogen and hydrogen sulphide, partial pressure of sulphide of hydrogen between 5000 and 71000 Pascal.
- Hydrogen sulfide can be either generated in the reaction chamber by hydrogenolysis of a sulfur compound in the presence of hydrogen (sulfide nascent hydrogen) such as thiols, organic sulphides, organic disulfides and the organic polysulfides, is introduced simultaneously with hydrogen.
- sulfide nascent hydrogen such as thiols, organic sulphides, organic disulfides and the organic polysulfides
- a hydrotreatment catalyst containing 18.2% by weight of molybdenum oxide and 3.8% by weight of cobalt oxide deposited on a high surface area alumina support (220 m 2 / g) is sulphurized at atmospheric pressure by a sulpho-reducing agent mixture.
- the sulphurization of the catalyst is obtained in two stages, the first being a controlled temperature rise phase (5 ° C./min), the second a 4 hour stage at the final sulphurization temperature chosen.
- the final sulphurization temperature may be either 400 ° C. or 500 ° C. After sulfurization, the catalyst is cooled under nitrogen flow to room temperature.
- the same oxide catalyst is loaded into the reactor of a gas oil hydrodesulfurization test unit operating under hydrogen pressure and in the liquid phase.
- the said catalyst Prior to activity measurement, the said catalyst is sulphurized (in situ mode) by a reducing sulpho mixture consisting of 5% volume of sulphide hydrogen and 95% hydrogen by gradually increasing the temperature (5 ° C / min), ambient (25 ° C) at 380 ° C. After a plateau of 11 hours at 380 ° C., the catalyst is cooled down to ambient temperature under nitrogen flow.
- Example 2 The same catalyst as that used in Example 1 is pre-impregnated at 90% of its impregnation volume with an atmospheric distillation diesel with an initial and final cutting point of 250 ° C. to 350 ° C. Before sulphidation treatment, a portion of solid is taken to analyze the total amount of carbon impregnated. The amount of carbon present on the prepreg solid is 28% by weight, corresponding to a molar ratio C / (Co + Mo) of 11.71. After leaching, in a reflux toluene soxhlet, the residual (non-extractable) carbon content present on the precarbonated solid is 0.2% by weight corresponding to a molar ratio C / (Co + Mo) of 0.48. which represents a leaching rate of 99.3%.
- Example 2 The same catalyst used in Example 1 is pre-impregnated at 90% of its impregnation volume with a vegetable oil (rapeseed oil). After a thermal treatment under nitrogen at 400 ° C. for 4 hours, a treatment intended to pyrolyze the organic molecule to release the lightest fragments and leave on the catalyst only a carbonaceous residue that is weakly hydrogenated and largely non-leachable with toluene. When hot, the catalyst is cooled to ambient temperature while maintaining it under nitrogen. Before the sulfurization treatment, part of the solid is removed to analyze the amount of carbon remaining on the oxide catalyst after the pyrolysis treatment.
- a vegetable oil rapeseed oil
- the amount of carbon present on the precarbonated solid is 4.9% by weight, corresponding to a molar ratio C / (Co + Mo) of 2.31.
- the residual (non-extractable) carbon content present on the precarbonated solid is 4.3% by weight, corresponding to a molar ratio C / (Co + Mo) of 2.02, which represents a leaching rate of 12.2%.
- the sulfurization in the gas oil hydrodesulfurization test unit is carried out on the precarbon oxide in the same conditions as those described in Example 1.
- Example 2 The same catalyst used in Example 1 is impregnated at 90% of its impregnation volume with a mineral oil (150 Neutral Solvent) with a density of 0.875 g / cm 3 . After pyrolysis treatment under a stream of nitrogen at 350 ° C. for 4 hours, a portion of the solid is taken to analyze the carbon content before and after leaching with toluene under reflux. The results of the carbon analysis before and after the leaching treatment, expressed relative to the precarbonated catalyst, are respectively 5.0% and 4.1% corresponding respectively to molar ratios C / (Co + Mo) of 2.49 and 1.94, which represents a leaching rate of 18%.
- a mineral oil 150 Neutral Solvent
- the temperature is gradually increased (5 ° C / min) up to 300 ° C.
- samples are taken in the gaseous effluents and analyzed by gas phase chromatography to measure the residual amount of thiophene, thus giving the conversion rate.
- the activity or specific rate of each catalyst is calculated from the conversion rate of the reagent, its molar flow rate and the mass of catalyst charged to the reactor.
- the relative activity is defined as the ratio between the specific velocities measured on the precarbonated catalysts (Example 3) and on the reference catalysts (Example 1) sulphurized at the same temperature.
- the results are shown in the following table.
- Relative activity (%) Reference 400 ° C 1.6 100% pre-carbonised 400 ° C 2.5 156%
- the activity or specific rate of each catalyst is calculated from the conversion rate of the reagent, its molar flow rate and the mass of catalyst charged to the reactor.
- the relative activity is defined as the ratio between the specific velocities measured on the precarbonated catalysts (Example 3) and on the reference catalysts (Example 1) sulphurized at the same temperature.
- the results are shown in the following table.
- Relative activity (%) Reference 400 ° C 1.8 100% pre-carbonised 400 ° C 2.0 111%
- the solid precarbonated references are sulphurized in the HDS gasoil test unit as described in Example 1.
- the unit is pressurized under 3 MPa (30 bar) of hydrogen.
- the test gas oil (initial cutting point 229 ° C. and final 383 ° C.) of density 0.850 containing 1.32% by weight of sulfur is introduced at an hourly volume velocity (VVH) of 8 h -1 .
- VVH hourly volume velocity
- Precarbonation allows to record a significant increase in activity compared to a conventional sulphidation of an oxide under H 2 SH 2 in the gas phase, the gain being even more noticeable when the sulphurization is carried out at high temperature.
- Pre-carbonation reduces the selectivity of cracking and isomerization products probably by neutralizing the acidic sites of the support. Coking rate on precarbonated products is much lower than on untreated oxides.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Description
Par la suite, ces catalyseurs seront dénommés " catalyseurs références ".
S/(Co+Mo) | Taux de sulfuration (%) | |
Sulfuration H2S-H2 (15/85) à 400°C | 1.70 | 104 % |
Sulfuration H2S-H2 (15/85) à 500°C | 1.70 | 104 % |
Avant traitement de sulfuration | Après traitement de sulfuration | |||
C/(Co+Mo) | C/(Co+Mo) | S/(Co+Mo) | Taux de sulfuration (%) | |
Sulfuration H2S-H2 (15/85) à 400°C | 11.71 | 0.92 | 1.69 | 103 % |
Sulfuration H2S-H2 (15/85) à 500°C | 11.71 | 0.66 | 1.71 | 104 % |
Avant traitement de sulfuration | Après traitement de sulfuration | |||
C/(Co+Mo) | C/(Co+Mo) | S/(Co+Mo) | Taux de sulfuration (%) | |
Sulfuration H2S-H2 (15/85) à 400°C | 2.31 | 1.72 | 1.63 | 99 % |
Sulfuration H2S-H2 (15/85) à 500°C | 2.31 | 1.58 | 1.69 | 103 % |
Avant traitement de sulfuration | Après traitement de sulfuration | |||
C/(Co+Mo) | C/(Co+Mo) | S/(Co+Mo) | Taux de sulfuration (%) | |
Sulfuration H2S-H2 (15/85) à 400°C | 2.49 | 1.16 | 1.66 | 101 % |
Sulfuration H2S-H2 (15/85) à 500°C | 2.49 | 1.08 | 1.69 | 103 % |
catalyseur | Température de sulfuration (°C) | Vitesse spécifique (10-6.mole.g-1.s-1) | Activité relative (%) |
Référence | 400°C | 1.6 | 100 % |
Précarboné | 400°C | 2.5 | 156 % |
Référence | 500°C | 1.6 | 100 % |
Précarboné | 500°C | 2.7 | 169 % |
Catalyseur | Température de sulfuration (°C) | Vitesse spécifique (10-7.mole.g-1.s-1) | Activité relative (%) |
Référence | 400°C | 1.8 | 100 % |
Précarboné | 400°C | 2,0 | 111 % |
Référence | 500°C | 1.7 | 100 % |
Précarboné | 500°C | 2.4 | 141 % |
Catalyseur | Température de sulfuration (°C) | C/(Co+Mo) Avant test tétraline | C/(Co+Mo) Après test tétraline | Sélectivité (%) Craquage & Isomérisation |
Référence | 400°C | 0 | 1.46 | 10 % |
Précarboné | 400°C | 1.72 | 1.72 | 4 % |
Référence | 500°C | 0 | 1.62 | 10 % |
Précarboné | 500°C | 1.58 | 1.58 | 4 % |
Temps en huile * (heure) | + 0 h | + 6 h | + 16 h | |||
Catalyseur | k | RWA | k | RWA | k | RWA |
Référence | 4.6 (ki) | 100 % | 4.2 | 91 % | 3.8 | 83 % |
Précarboné | 6.0 | 130 % | 5.2 | 113 % | 5.1 | 111 % |
Claims (7)
- Procédé de présulfuration d'un catalyseur d'hydroconversion d'hydrocarbures en présence d'hydrogène et d'au moins un composé sulfuré, ledit catalyseur comprenant un support oxyde sur lequel est déposé au moins un élément des groupes VIII et VI, procédé mis en oeuvre ex-situ dans lequel le catalyseur est précarboné avant le traitement de présulfuration, la précarbonation comportant l'imprégnation à température ambiante avec un composé carboné liquide suivie d'un traitement thermique (ou pyrolyse) sous gaz inerte à une température comprise entre 300 et 650°C de manière à déposer dans les pores du catalyseur un composé carboné résiduel en majeure partie non lixiviable au toluène à reflux, la teneur en carbone résiduel étant de 2-10% pds par rapport à l'oxyde.
- Procédé selon la revendication 1 dans lequel le traitement thermique est effectué à 300-500°C
- Procédé selon l'une des revendications précédentes dans lequel l'étape de sulfuration est réalisée à pression atmosphérique dans un réacteur chauffé à 200-600°C en présence d'un mélange sulfo réducteur.
- Procédé selon l'une des revendications précédentes dans lequel le composé liquide carboné d'imprégnation a un point d'ébullition supérieur à 200°C.
- Procédé selon l'une des revendications précédentes dans lequel le composé liquide carboné d'imprégnation est choisi dans le groupe constitué par les hydrocarbures paraffiniques, naphténiques, ou aliphatiques, les composés organiques oxygénés.
- Procédé selon l'une des revendications précédentes dans lequel le composé carboné d'imprégnation est une huile végétale.
- Procédé selon l'une des revendications précédentes pour lequel le taux de lixiviation au toluène à reflux du composé carboné résiduel est inférieur à 40%.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9910577A FR2797594B1 (fr) | 1999-08-17 | 1999-08-17 | Precarbonation de catalyseur d'hydrotraitement |
FR9910577 | 1999-08-17 |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1077085A1 EP1077085A1 (fr) | 2001-02-21 |
EP1077085B1 true EP1077085B1 (fr) | 2005-11-16 |
Family
ID=9549202
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP00402216A Expired - Lifetime EP1077085B1 (fr) | 1999-08-17 | 2000-08-03 | Précarbonation de catalyseur d'hydrotraitement |
Country Status (8)
Country | Link |
---|---|
US (1) | US6559092B1 (fr) |
EP (1) | EP1077085B1 (fr) |
JP (1) | JP4866500B2 (fr) |
AT (1) | ATE309863T1 (fr) |
CA (1) | CA2316675C (fr) |
DE (1) | DE60024004T2 (fr) |
FR (1) | FR2797594B1 (fr) |
SG (1) | SG85725A1 (fr) |
Families Citing this family (19)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP4156859B2 (ja) * | 2001-06-20 | 2008-09-24 | コスモ石油株式会社 | 軽油の水素化処理触媒及びその製造方法並びに軽油の水素化処理方法 |
WO2004054712A1 (fr) * | 2002-12-18 | 2004-07-01 | Cosmo Oil Co., Ltd. | Catalyseur d'hydrotraitement pour carburant diesel, procede de production de ce catalyseur et procede d'hydrotraitement de carburant diesel |
WO2010142350A1 (fr) | 2009-06-12 | 2010-12-16 | Aggregate Energy, Llc. | Catalyseur comprenant un métal et un composant complémentaire et procédé pour l'hydrogénation de produits organiques contenant de l'oxygène |
FR2949982B1 (fr) | 2009-09-11 | 2011-12-09 | Eurecat Sa | Procede de sulfuration de catalyseurs de traitement d'hydrocarbures |
FR2949981B1 (fr) | 2009-09-11 | 2012-10-12 | Eurecat Sa | Procede de sulfuration de catalyseurs de traitement d'hydrocarbures |
US8673805B2 (en) | 2011-02-17 | 2014-03-18 | Phillips 66 Company | MoS2 catalyst for the conversion of sugar alcohol to hydrocarbons |
CN103657740B (zh) * | 2012-09-19 | 2015-05-20 | 中国石油化工股份有限公司 | 一种耐硫变换催化剂分步硫化方法 |
CN103657741B (zh) * | 2012-09-19 | 2015-10-14 | 中国石油化工股份有限公司 | 一种耐硫变换催化剂循环快速预硫化及利用其进行分段预硫化方法 |
EP3326716A1 (fr) * | 2013-10-31 | 2018-05-30 | Reactor Resources, LLC | Procédés et systèmes de sulfuration, de passivation et de cokéfaction de catalyseur in situ |
CN105582963B (zh) * | 2014-10-22 | 2017-11-24 | 中国石油化工股份有限公司 | 一种硫化型汽油选择性加氢脱硫催化剂的制备方法 |
CN105586072B (zh) * | 2014-10-22 | 2017-09-29 | 中国石油化工股份有限公司 | 一种加氢脱硫催化剂预硫化方法 |
CN106732666B (zh) * | 2015-11-20 | 2019-01-25 | 中国石油化工股份有限公司 | 一次成型的大孔硫化型加氢催化剂的制备方法 |
SG11202000663PA (en) | 2017-07-26 | 2020-02-27 | Chem32 Llc | Methods of treating and sulfiding hydroconversion catalysts |
CN109777475B (zh) * | 2017-11-14 | 2021-08-31 | 中国石油化工股份有限公司 | 一种加氢裂化催化剂快速的开工方法 |
CN109777476B (zh) * | 2017-11-14 | 2022-03-08 | 中国石油化工股份有限公司 | 一种加氢裂化催化剂安全的开工方法 |
CN109777480B (zh) * | 2017-11-14 | 2021-08-31 | 中国石油化工股份有限公司 | 一种加氢裂化催化剂高效的开工方法 |
WO2021001474A1 (fr) | 2019-07-04 | 2021-01-07 | Haldor Topsøe A/S | Sulfuration en phase gazeuse de catalyseurs d'hydrotraitement et d'hydrocraquage |
FR3116740A1 (fr) * | 2020-11-27 | 2022-06-03 | IFP Energies Nouvelles | Procédé de préparation d’un catalyseur d’hydrodésulfuration d’une coupe essence comprenant un métal du groupe VIB, un métal du groupe VIII et du carbone graphitique |
US20220212182A1 (en) * | 2021-01-04 | 2022-07-07 | Saudi Arabian Oil Company | Method to coat hydroscopic catalyst particles to prevent water adsorption |
Family Cites Families (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2548205B1 (fr) * | 1983-06-30 | 1985-11-29 | Eurecat Europ Retrait Catalys | Procede de presulfuration de catalyseur de traitement d'hydrocarbures |
DE3562987D1 (en) * | 1984-10-30 | 1988-07-07 | Eurecat Europ Retrait Catalys | Method for presulfiding a catalyst for the treatment of hydrocarbons |
FR2627105B3 (fr) * | 1988-02-16 | 1990-06-08 | Inst Francais Du Petrole | Procede de presulfuration de catalyseur de traitement d'hydrocarbures |
JPH02237644A (ja) * | 1989-03-09 | 1990-09-20 | Suehiko Yoshitomi | 触媒の製造法 |
FR2689420B1 (fr) * | 1992-04-01 | 1994-06-17 | Eurecat Europ Retrait Catalys | Procede de presulfuration de catalyseur de traitement d'hydrocarbures. |
US5489722A (en) * | 1992-04-27 | 1996-02-06 | Sun Company, Inc. (R&M) | Dehydrogenation processes using catalysts comprising catalytic metal on a nonacidic support |
US5462904A (en) * | 1992-04-27 | 1995-10-31 | Sun Company, Inc. (R&M) | Process of making dehydrogenation catalysts by oxidizing and sulfiding catalytic metal on a nonacidic support |
US5733518A (en) * | 1992-04-27 | 1998-03-31 | Sun Company, Inc. (R&M) | Process and catalyst for dehydrogenation of organic compounds |
FR2725381B1 (fr) * | 1994-10-07 | 1996-12-13 | Eurecat Europ Retrait Catalys | Procede de pretraitement hors site d'un catalyseur de traitement d'hydrocarbures |
JP3291164B2 (ja) * | 1995-06-02 | 2002-06-10 | 日石三菱株式会社 | 接触分解ガソリンの脱硫方法 |
FR2743512B1 (fr) * | 1996-01-17 | 1998-03-13 | Eurecat Europ Retrait Catalys | Procede d'incorporation de soufre dans la porosite d'un catalyseur de traitement d'hydrocarbures |
US5922638A (en) * | 1996-06-12 | 1999-07-13 | Europeene De Retraitement De Catalyseurs Eurecat | Process for presulfurizing hydrotreatment catalysts |
-
1999
- 1999-08-17 FR FR9910577A patent/FR2797594B1/fr not_active Expired - Lifetime
-
2000
- 2000-08-03 DE DE60024004T patent/DE60024004T2/de not_active Expired - Lifetime
- 2000-08-03 AT AT00402216T patent/ATE309863T1/de not_active IP Right Cessation
- 2000-08-03 EP EP00402216A patent/EP1077085B1/fr not_active Expired - Lifetime
- 2000-08-15 CA CA002316675A patent/CA2316675C/fr not_active Expired - Lifetime
- 2000-08-17 SG SG200004565A patent/SG85725A1/en unknown
- 2000-08-17 US US09/639,880 patent/US6559092B1/en not_active Expired - Lifetime
- 2000-08-17 JP JP2000247247A patent/JP4866500B2/ja not_active Expired - Lifetime
Also Published As
Publication number | Publication date |
---|---|
DE60024004D1 (de) | 2005-12-22 |
CA2316675A1 (fr) | 2001-02-17 |
DE60024004T2 (de) | 2006-06-08 |
FR2797594A1 (fr) | 2001-02-23 |
FR2797594B1 (fr) | 2001-09-21 |
ATE309863T1 (de) | 2005-12-15 |
JP2001113178A (ja) | 2001-04-24 |
CA2316675C (fr) | 2009-01-27 |
US6559092B1 (en) | 2003-05-06 |
SG85725A1 (en) | 2002-01-15 |
EP1077085A1 (fr) | 2001-02-21 |
JP4866500B2 (ja) | 2012-02-01 |
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